RU2159896C2 - Fluidized-bed thermal reaction unit - Google Patents

Abstract

FIELD: burning or gasifying combustible materials containing non-combustible components. SUBSTANCE: unit has slight-dissipation plate, heavy-dissipation plate, and auxiliary dissipation plate each provided with great number of holes to admit fluidized gas and with outlet arranged between auxiliary dissipation plate and heavy-dissipation one to discharge non-combustible components. Some portion of fluidized gas is admitted through outlet for non-combustible components or the latter is made horizontally open. In this way, continuous circulating flow is organized at furnace bottom in fluidized bed. Both slight- dissipation plate and auxiliary dissipation one have their surfaces inclined downward towards non-combustible component outlet. Heavy-dissipation plate is inclined upwards gradually rising as it goes away from point of non- combustible component outlet. In this way, non-combustible components are continuously discharged and do not settled down inside furnace. EFFECT: improved efficiency of burning and gasifying processes. 8 cl, 11 dwg

Description

 The present invention relates to a thermal fluidized bed reaction device suitable, for example, for use as a fluidized bed combustion device, a fluidized bed gasification device, or a fluidized bed carbonization system in which a solid combustible substance containing non-combustible components, for example industrial waste, municipal waste or coal is burned or gasified in a fluidized bed furnace. In particular, the present invention relates to a thermal fluidized bed reaction device that allows the non-combustible components to be uniformly removed from the fluidized bed furnace without being deposited on any part of the furnace, uniformly and efficiently burning or gasifying the aforementioned combustible material and stably recovering a product such as thermal energy or combustible gas.

 With the development of the economy, the amount of solid combustible material containing non-combustible components, such as industrial waste or municipal waste, has steadily increased. Such a combustible substance contains a large, albeit variable in quality, shape, etc., amount of energy and at the same time contains a large amount of non-combustible substance of irregular shape. For this reason, it is difficult to stably burn such combustible substances in order to efficiently utilize energy or to gasify them in order to produce combustible gas.

 JP-A-4-214110 (Publication (KOKAI) N4-214110 of the Unexamined Japanese Patent Application) describes a fluidized bed incinerator in which waste containing a non-combustible material is burned in a fluidized bed furnace and when incinerated the ovens uniformly remove non-combustible material, thereby achieving stable combustion. In the combustion device shown in FIG. 1 of this publication, a hole 50 for unloading a non-combustible substance is formed between the air diffusion plate 40 and the furnace wall, and the upper surface 44 of the air diffusion plate is inclined so that the side of the upper surface 44, which is closer to the discharge hole 50 of the non-combustible substance, is located at a lower level and an increased amount of air flows to the lower side of the air dispersion plate 40 in comparison with the increased side of the plate 40. However, at a lower side not the plate 40 air dispersion occurs when this vigorous fluidization of the fluidized bed by a large amount of supplied air. Therefore, the fluidized bed exhibits properties similar to those of liquids. Accordingly, in the fluidized bed, substances with a higher specific gravity than that of the fluidized bed are deposited, while substances with a lower specific gravity than that of the fluidized bed float in it. That is, the so-called gravitational separation occurs. For this reason, non-combustible components of a large specific gravity settle and, as a result, are undesirably deposited on the bottom of the furnace until they reach the discharge opening 50 of the non-combustible substance. Moreover, since the non-combustible substance discharge opening 50 that is not provided with a fluidizing gas is open in the plane of the furnace bottom surface, the portion of the fluidized bed that lies above the non-combustible substance discharge opening 50 is unstabilized.

 The heat treatment device shown in FIG. 11 in JP-A-4-214110, has air diffusion plates 90a and 90b with downward inclined surfaces extending from the center of the furnace to two non-combustible material discharge openings 95a and 95b, respectively, and air diffusion plates 95c and 95d with downwardly inclined surfaces, going from the walls of the side surface, respectively, to the holes 95a and 95b unloading non-combustible substances. An increased amount of air comes from air diffusion plates located close to the discharge openings of the non-combustible substance than from other sections through the air chambers 93c and 93e. The fluidized bed, which is vigorously fluidized by a large amount of air, exhibits properties similar to those of liquids. Thus, the so-called gravitational separation occurs in the fluidized bed. That is, substances with a higher specific gravity than the fluidized bed sediment, while substances with a lower specific gravity than the fluidized bed float in it.

 As a result of the settling of non-combustible components having a large specific gravity, non-combustible components are deposited on the bottom of the furnace until the openings 95a and 95b for unloading of non-combustible material are reached. This makes it difficult to uniformly unload a non-combustible substance. In addition, there is a gradual deterioration in mobility, and ultimately comes the moment when the device can no longer work. Meanwhile, the discharge openings of the non-combustible substance into which the fluidizing gas is blown are open in the plane of the surface of the furnace bottom. For this reason, a fixed bed that does not turn out to be fluidized is formed near and above each discharge opening of a non-combustible substance. The fixed bed disrupts the formation of a smoothly circulating flow in the fluidized bed. This prevents the dispersion and mixing of fuel in the fluidized bed, as well as the unloading of non-combustible components.

 JP-A-4-214110 (Japanese Patent Publication No. 5-19044) describes a fluidized bed furnace for burning waste containing non-combustible material such as metal shavings, soil and stone. Under this fluidized bed furnace, this publication has a downward inclined surface leading to a non-combustible material discharge opening 5 located in the center of the hearth, and the fluidizing air is supplied so that the amount of fluidizing air per unit area of the hearth is large near the non-combustible discharge opening substances and stepwise fell towards the side wall of the furnace. Accordingly, a circulating flow acts in the fluidized bed, which goes up to the discharge hole 5 of the non-combustible substance located in the center of the hearth, and which goes down near the side wall of the furnace. Meanwhile, the waste is fed into an area located directly above the hole 5 for unloading a non-combustible substance. Consequently, the waste feed is blown upward and burned in the upper part of the fluidized bed or they are scattered to the protruding side wall and burn there. Thus, the combustion efficiency in the fluidized bed is undesirably reduced.

 In the case where the waste is introduced from the side of the furnace side wall to eliminate the problems noted above, the waste is favorably dispersed and mixed in the fluidized bed in a downward flow, and the combustion efficiency in the bed is improved. However, since a large amount of air is supplied to a location located up to the discharge opening 5 of the non-combustible substance, a fluidized bed that is vigorously fluidized with a large amount of air exhibits properties similar to those of liquids, as in the case of JP-A-4-214110. In this situation, substances with a higher specific gravity than the fluidized bed settle, whereas substances with a lower specific gravity than the fluidized bed float. That is, the so-called gravitational separation occurs. For this reason, non-combustible components of high specific gravity settle and, as a result, are deposited at the bottom of the furnace until the discharge opening of the non-combustible substance is reached. The foregoing makes it difficult to uniformly unload non-combustible components. These difficulties regarding the unloading of non-combustible components also arise in a gasification device in a fluidized bed having a similar fluidized bed.

 The closest analogue of the invention is a thermal fluidized bed reaction device according to EP 0047159 A1, cl. F 23 C 11/02, 03/10/1982.

 Known thermal reaction device for burning in a fluidized bed combustible substances containing non-combustible components, includes a fluidized bed furnace, a weak dispersion plate and a strong dispersion plate, each of which is made with a large number of holes for supplying fluidizing gas located in the bottom of the furnace, an opening for outputting non-combustible components, made between a weak diffusion plate and a strong dispersion plate, a plate for supplying a part of the fluidizing gas through an opening for discharging non-combustible components in such a way as to allow the removal of large particles, an opening for supplying combustible material to the region above the weak dispersion plate, the weak dispersion plate being able to supply fluidizing gas so that a relatively low fluidizing velocity is established at the fluid and a downward flow is formed fluid, and has a surface inclined downward towards the place of output of non-combustible components, and a strong dispersion plate has a method It is possible to supply fluidizing gas in such a way that a relatively high fluidization rate is established for the fluid and an upward flow of fluid is formed.

 The general objective of the present invention is to eliminate the difficulties described above inherent in known methods and to develop a thermal fluidized bed reaction device in which a solid combustible substance containing non-combustible components, such as industrial waste, municipal waste or coal, is burned in a furnace with fluidized bed and in which non-combustible components with a high specific gravity can be uniformly removed from the fluidized-bed furnace, thereby eliminating the possibility of deposits of non-combustible components comrade to some part of the furnace and stabilizing fluidization in the furnace, which thereby gives the possibility of combustibles to burn or gasify uniformly.

 Supported by a moving bed (in which the fluid is in transition between the fixed bed and the fluidized bed), non-combustible components of a large specific gravity, such as iron, cannot settle, but can move in the horizontal direction. In a fluidized bed, in which, however, vigorous fluidization occurs, such non-combustible components quickly settle and separate, as a result of which their advancement and discharge are difficult. In view of the foregoing, it is an object of the present invention, in particular, to provide a thermal fluidized bed reaction device in which a combustible material containing non-combustible components that is introduced into the furnace is transferred directly to the place of non-combustible component removal by the moving bed and the fluid is vigorously fluidized near the outlet non-combustible components, resulting in rapid combustion or gasification of combustible components, as well as the possibility of combustible components a large specific gravity is separated from the combustible components by settling and discharged through the outlet of the non-combustible components.

 Another objective of the present invention is the development of a thermal fluidized bed reaction device in which the flow of fluidized gas is not interrupted by the removal of non-combustible components, and the main fluidized bed and the main circulating fluid flow that are formed in the furnace are stabilized, thereby enabling favorable combustion or gasification of a combustible substance.

 And another objective of the present invention is the development of a thermal fluidized bed reaction device in which, while a combustible substance containing non-combustible components that enters the furnace is advanced in a downward flow and in a horizontal fluid flow, the formation of an upper fluidized bed under the influence of pneumatic elutriation bed of small specific gravity and high concentration of combustible components and lower fluidized bed of high relative density and high concentrations of non-combustible components, and the upper layer with a high concentration of combustible components is mixed in an upward flow, passing above the place of unloading of non-combustible components, and then undergoes further circulation, while non-combustible components and fluid located in the lower fluidized bed of a large specific gravity and high concentration of non-combustible components are mainly removed from the furnace through the place of removal of non-combustible components.

 A further object of the present invention is to provide a thermal fluidized bed reaction device that is able to efficiently remove noncombustible components from the furnace and stably extract thermal energy from a heat recovery device located in a sub-fluidized bed that is formed separately from the main fluidized bed. Other objectives of the present invention will become apparent from the drawings, the description of the options for its implementation and the attached claims.

 Means for achieving the objectives of the invention.

 The present invention provides a thermal fluidized bed reaction device in which a combustible material containing non-combustible components is burned or gasified in a fluidized bed furnace. In the proposed device, in the bottom of the furnace for forming the main fluidized bed, a weak diffusion plate and a strong dispersion plate are installed, each of which has a large number of holes for supplying a fluidizing gas, and an elongated or annular exit for removing noncombustible components is placed between the plates of weak and strong dispersion. A hole for supplying the combustible substance to the fluidized bed furnace is arranged so that the combustible substance can fall into the region above the weak diffusion plate. The weak dispersion plate has the ability to deliver fluidizing gas so that a relatively small fluidizing velocity of the fluid is obtained and a downward flow of fluid is formed, and it has a downward inclined surface leading to the place of withdrawal of non-combustible components.

 The strong diffusion plate has the ability to deliver fluidizing gas so that a relatively high fluidizing velocity is communicated to the fluid and an upward flow of fluid is generated. The fluid forms the main circulating flow, which alternately moves in the outgoing and ascending directions. A part of the fluidizing gas comes from the discharge outlet of non-combustible components through an additional diffusion plate having a large number of fluid supply ports, so that fluidization occurs near the outlet of non-combustible components, as a result of which the fluidized medium is connected to the main fluidized bed, which stabilizes the main circulating flow. The proposed technical fluidized-bed reaction device is intended for burning or gasifying a combustible substance by using air, oxygen, exhaust gas or a mixture of these gases as a fluidizing gas and controlling the proportion of oxidizing gas, for example, air or oxygen, supplied with the combustible substance.

 The combustible material coming from the fuel supply opening moves down to the bottom of the furnace along with a downward flow of fluid and then moves horizontally along the downwardly inclined surface of the weak diffusion plate. During horizontal movement along a downward inclined surface, the combustible substance undergoes pneumatic elutriation from the bottom of the ascending fluidizing gas, which is accompanied by the formation of an upper fluidized bed of low specific gravity and a high concentration of combustible components and a lower fluidized bed of high specific gravity and a high concentration of non-combustible components near the place of removal of non-combustible components. The upper fluidized bed with a high concentration of combustible components is mixed in an upward flow of fluid passing over the outlet of the output of non-combustible components, and then continues to circulate, burning. Fluid and noncombustible components located in the lower fluidized bed are predominantly removed from the outlet of the noncombustible components.

 It is advisable that the auxiliary diffusion plate having a large number of fluidizing gas supply openings is located between the weak diffusion plate and the place of removal of non-combustible components. The auxiliary diffusion plate is capable of supplying fluidizing gas in such a way that a relatively high fluidizing velocity is imparted to the fluid, and it has a downward inclined surface with a steeper slope than that of the weak diffusion plate, in the region between the lower edge of the weak diffusion plate and the place of removal of non-combustible components, so that the downward inclined surface passes to the place of removal of non-combustible components. In addition, an inclined wall is located above the strong scattering plate, necessary to return the fluidizing gas and fluid rising above the strong scattering plate, back to the area located above the weak scattering plate, i.e. in the central part of the furnace. The protruding side wall is located above the inclined wall. The strong dispersion plate has an upward inclined surface that gradually rises with distance from the place of withdrawal of non-combustible components, and it is located so that the fluidizing velocity gradually increases with distance from the place of exit of non-combustible components.

 In addition, a heat recovery chamber is formed between the inclined wall and the side wall of the furnace. The heat recovery chamber communicates with the central part of the furnace at the upper and lower ends of the inclined wall. A heat recovery device is disposed in a heat recovery chamber. A third diffusion plate is positioned between the strong diffusion plate and the side wall of the furnace so that the third diffusion plate is in contact with the outer edge of the strong diffusion plate. The third diffusion plate is capable of delivering a fluidizing gas in such a way that a relatively low fluidizing velocity is imparted to the fluid in the heat recovery chamber, and it has an inclined surface with the same inclination as the strong diffusion plate. The flat configuration of the bottom of the furnace can be rectangular or round. The rectangular bottom of the furnace is formed by placing a rectangular plate of weak dispersion parallel to the location of the opening of the outlet of non-combustible components and a plate of strong dispersion, or by arranging rectangular holes of the discharge of non-combustible components and rectangular plates of strong dispersion symmetrically with respect to the edge of a rectangular plate of weak dispersion with an angular section. The round bottom of the furnace is formed by the installation of a conical plate of weak dispersion, which is high in the center and low at the peripheral edge, and the place of output of non-combustible components is configured to form a set of many partially annular portions concentrically relative to the plate of weak dispersion, and using the ring plate of strong dispersion.

 In yet another embodiment of the present invention, a thermal fluidized bed reaction device in which a combustible material containing non-combustible components is burned or gasified in a furnace bed has a weak diffusion plate, an auxiliary diffusion plate, and a strong dispersion plate, each of which contains a large number of fluidizing gas supply openings, and a place for removing non-combustible components is located between the auxiliary diffusion plate and a strong diffusion plate. A hole for introducing a combustible substance is located above the weak scattering plate to ensure that the combustible substance is discharged into the region above the weak dispersion plate. The weak diffusion plate has the ability to supply fluidizing gas so that a relatively low fluidizing velocity is imparted to the fluid, and it has a downward inclined surface extending toward the outlet of the non-combustible components.

 The auxiliary diffusion plate has the ability to deliver fluidizing gas so that the fluid is given a relatively high fluidizing velocity and it has a sloping surface with a steeper slope than that of the weak diffusion plate, in the region between the lower edge of the weak diffusion plate and the place of removal of non-combustible components, so that the downward sloping surface goes to the place of removal of non-combustible components. The strong diffusion plate has the ability to supply fluidizing gas so that it imparts a relatively high fluidizing velocity to the fluid and forms an upward flow of fluid. The lower edge of the downward sloping surface of the auxiliary diffusion plate covers in the horizontal direction the edge of the adjacent strong diffusion plate, and these edges recede from each other in the vertical direction. The outlet for the removal of non-combustible components is open in the vertical gap between the two edges. That is, the exit is horizontally open.

 It is advisable that an inclined wall is located above the strong scattering plate, which ensures the return of fluidized gas and fluid ascending from the strong scattering plate to the region above the weak scattering plate, i.e., to the central part of the furnace. The protruding side is located above the inclined wall. The strong dispersion plate has an upwardly inclined surface that gradually rises away from the place of withdrawal of non-combustible components, and it is positioned in such a way that the fluidizing velocity gradually increases with distance from the place of withdrawal of non-combustible components. A heat recovery chamber is formed in the region between the inclined wall and the side wall of the furnace. The heat recovery chamber communicates with the central part of the furnace at the upper and lower ends of the inclined wall. A heat recovery device is disposed in a heat recovery chamber. A third diffusion plate is positioned between the strong diffusion plate and the side wall of the furnace so that the third diffusion plate is in contact with the outer edge of the strong diffusion plate. The third diffusion plate has the ability to supply fluidizing gas in such a way that a relatively low fluidized velocity is communicated in the heat recovery chamber to the fluid, and it has an inclined surface with approximately the same inclination as the strong diffusion plate.

 The flat configuration of the bottom of the furnace can be rectangular or round. The rectangular bottom of the furnace is formed by the parallel arrangement of a rectangular plate of weak dispersion and a plate of strong dispersion or the arrangement of rectangular plates of weak dispersion and rectangular plates of strong dispersion symmetrically with respect to the edge of a rectangular plate of weak dispersion with an angular section. The round bottom of the furnace is formed using a conical weak diffusion plate, an inverted cone-shaped strong diffusion plate mounted concentrically with respect to the weak diffusion plate, and using an opening for removing non-combustible components in the form of a vertical gap between the outer peripheral edge of the weak diffusion plate and the inner peripheral edge of the strong diffusion plate .

 In the proposed thermal fluidized bed reaction device, the fluidizing gas supplied through the weak diffusion plate imparts a relatively low fluidizing velocity to the fluid so that a downward flow of fluid is formed, and the fluidizing gas supplied through the strong diffusion plate imparts a relatively high fluidizing velocity to the fluid, so that an upward flow of fluid is formed. In this way, a main fluidized bed with upward and downward flows is obtained. After moving downward in a downward flow, the fluid is directed along the downwardly inclined surface of the weak diffusion plate and converted into an upward flow near the strong diffusion plate. The fluid, having reached the top of the fluidized bed, is carried to the central part of the furnace and then made downward again, thereby forming a circulating stream that circulates in the main fluidized bed.

 By supplying a fluidizing gas through an additional diffusion plate, which is located in the outlet of the outlet of non-combustible components, so that a relatively high fluidizing speed is reported, the fluid is energetically fluidized near and above the outlet of the outlet of non-combustible components. Therefore, the fluidizing medium above the location of the hole for the output of non-combustible components also forms a fluidized bed, and not a fixed bed. Thus, the fluidization zone extends from the location of the weak diffusion plate to the location of the strong diffusion plate, and the main circulating flow that descends in the weak fluidization zone and rises in the strong fluidization zone is made stable without gaps. The inclined wall above the strong diffusion plate reflects the fluidizing gas and fluid rising upward from the strong diffusion plate to the central part of the furnace, contributing to the formation of the main circulating flow.

 The combustible substance is discharged into the region located above the weak dispersion plate from the inlet of the combustible substance. The region above the weak diffusion plate is made by the region of soft fluidization and is in the state of the moving bed, which is characterized by an intermediate state between the states of the fixed bed and the fluidized bed. In a moving bed, combustible matter and noncombustible components are suspended in a fluid. Consequently, the combustible material and noncombustible components are taken together together by a circulating fluidized bed flow and then move horizontally into the fluidization zone above the strong dispersion plate, where the fluidizing velocity is high. However, the combustible substance and noncombustible components are in a state of soft fluidization, although they are suspended in the fluid. Therefore, while the combustible substance and noncombustible components move horizontally, the so-called gravitational separation slowly occurs. That is, substances with a specific gravity higher than that of the moving layer gradually settle, whereas substances with a lower specific gravity than that of the moving layer float. As a result, the combustible substance of small specific gravity moves upward, while the noncombustible components of large specific gravity move downward, and thus, the upper fluidized bed with a high concentration of combustible components and the lower fluidized bed with a high concentration of combustible components.

 The upper fluidized bed with a low specific gravity and a high concentration of combustible components is mixed in an upward fluid flow, passing above the place of removal of non-combustible components, and in the case of a combustion device, the upper fluidized bed is satisfactorily burned in an upward flow of an oxidizing atmosphere having a high fluidizing velocity. Since the upper fluidized bed has a relatively low content of non-combustible material, it burns favorably in the upward flow. In the case of a gasification device, the combustible substance partially burns out and effectively thermally decomposes in the upper fluidized bed. Thus, exceptionally good gasification occurs.

 The lower fluidized bed with a high specific gravity and a high concentration of non-combustible components is directed to the downwardly inclined surface of the weak diffusion plate to get to the place of removal of non-combustible components, which is located between the weak diffusion plate and the strong dispersion plate. Thus, fluid and non-combustible components are sampled from the outlet of the non-combustible component outlet. That is, since the fluid above the weak scattering plate is in the state of the moving layer, even non-combustible components with an extremely large specific gravity, such as iron, are supported by the moving layer and are shifted to the vicinity of the outlet of the non-combustible components. Accordingly, no deposits of non-combustible components are formed at the bottom of the furnace. Meanwhile, the fluidizing gas is supplied through a diffusion plate installed at the place of discharge of non-combustible components to set a relatively high fluidizing velocity, which ensures energetic fluidization of the fluid near and above the entrance to the outlet of the output of non-combustible components.

 Therefore, the fluid near and above the entrance to the outlet of the outlet of non-combustible components is in a state of vigorous fluidization, and not in the state of either a fixed layer or a moving layer. Therefore, the fluidized bed exhibits properties similar to those of liquids. Accordingly, the so-called gravitational separation easily occurs in the fluidized bed. That is, substances with a specific gravity higher than that of the fluidized bed are deposited, while substances with a lower specific gravity than that of the fluidized bed are floating up in the fluidized bed. Accordingly, non-combustible components with a high specific gravity quickly settle towards the place of removal of non-combustible components: therefore, the unloading of non-combustible components is extremely easy and uniform. Since non-combustible components are uniformly and effectively removed from the furnace, they do not interfere with the flow of combustion or gasification in the furnace. Since combustible components and non-combustible components are separated by pneumatic elutriation and almost only non-combustible components are removed, the loss of heat from the furnace is small, and the handling of unloaded non-combustible components is also relatively easy.

 It is advisable that the auxiliary diffusion plate with a steeper slope than that of the weak diffusion plate be used to supply a fluidizing gas with a relatively high fluidizing velocity, which would thereby facilitate the transition of the movable layer displaced from the weak diffusion plate to the state of the fluidized bed . Thus, the process of separating non-combustible components by pneumatic elutriation rapidly progresses, and, in particular, non-combustible components with a high specific gravity, for example iron, are deposited on the auxiliary dispersion plate. However, since the auxiliary diffusion plate has a steep slope, such non-combustible components of large specific gravity are sent without delay to the outlet of the output of non-combustible components. The strong dispersion plate is installed in such a way that the fluidizing velocity gradually increases with increasing distance from the place of withdrawal of non-combustible components. Thus, the strong diffusion plate contributes to the formation of the main circulating flow centered on the central part of the furnace.

 The third diffusion plate reports a relatively low fluidizing velocity of the fluid in the heat recovery chamber, so that a movable layer forms which descends in the heat recovery chamber. Part of the fluid in the upper part of the upward flow, which is reflected to the central part of the furnace by the inclined wall, enters the heat recovery chamber through the upper end of the inclined wall and descends in the form of a movable layer. After being cooled by heat exchange with a heat recovery device, the fluid flows along the third scattering plate into the region located above the strong scattering plate, and then mixes in the upward flow and is heated by the heat of combustion in the upward flow. Thus, the subcirculating fluid flow is generated by the upward flow in the heat recovery chamber and the upward flow in the main combustion chamber, and the heat of combustion in the fluidized bed furnace is extracted by the heat recovery device in the heat recovery chamber. As shown in FIG. 10, the total heat transfer coefficient of the heat recovery device varies greatly with the fluidization rate. Therefore, the amount of heat extracted can be easily controlled by changing the transmission rate of the fluidizing gas through the third diffusion plate.

 With a rectangular rectangular configuration, the design and manufacture of a fluidized-bed furnace can be relatively easy. However, if the furnace’s flat configuration is round, then it becomes possible to increase the discharge resistance at the side wall of the fluidized bed furnace and it becomes possible to prevent leakage of odorous and harmful gas from combustible waste by lowering the pressure in the furnace or, conversely, to obtain high gas pressure capable of driving a turbine by increasing the pressure in the furnace.

 In yet another embodiment of the present invention, when considering the diffusion plates located around the outlet of the non-combustible components, the bottom edge of one diffusion plate in plan substantially contacts the lower edge of another diffusion plate, and these edges recede from each other in the vertical direction. The place of output of non-combustible components falls on the vertical gap between these two edges. Thus, the area above the place of removal of non-combustible components can be fluidized without installing a scattering plate on the inner surface of the place of output of non-combustible components. As a result, the fluidization zone extends from the weak diffusion plate to the strong diffusion plate, and the circulating flow that flows down in the weak fluidization zone and rises in the strong fluidization zone is stable without any tendency to breaks.

 FIG. 1 is a vertical sectional view schematically illustrating an essential part of a thermal fluidized bed reaction device according to a first embodiment of the present invention.

 FIG. 2 is a vertical sectional view schematically illustrating an essential part of a thermal fluidized bed reaction apparatus according to a second embodiment of the present invention.

 FIG. 3 is a vertical sectional view schematically illustrating an essential part of a thermal fluidized bed reaction apparatus according to a third embodiment of the present invention.

 FIG. 4 is a vertical sectional view schematically illustrating an essential part of a thermal fluidized bed reaction apparatus according to a fourth embodiment of the present invention.

 FIG. 5 is a spatial view schematically showing the bottom of a furnace at a thermal reaction device with a fluidized bed according to a fifth embodiment of the present invention.

 FIG. 6 is a plan view schematically showing the bottom of the furnace of a thermal reaction device with a fluidized bed shown in FIG. 5.

 FIG. 7 is a vertical sectional view schematically showing the bottom of the furnace of a thermal reaction device with the fluidized bed shown in FIG. 5.

 FIG. 8 is a spatial view schematically showing the bottom of a furnace of a thermal reaction device with a fluidized bed according to a sixth embodiment of the present invention.

 FIG. 9 is a spatial view schematically showing the bottom of a furnace of a thermal reaction device with a fluidized bed according to a seventh embodiment of the present invention.

 FIG. 10 is a graph depicting the relationship between the total heat transfer coefficient of a fluidizing heat recovery apparatus of a fluidizing gas supplied through a third diffusion plate in a thermal reaction apparatus with a fluidized bed according to the present invention.

 FIG. 11 is a cross-sectional view schematically illustrating a bottom of a furnace of a thermal fluidized bed reaction apparatus according to an eighth embodiment of the present invention.

 Next, a number of embodiments of the present invention will be described with reference to the drawings. However, the technical capabilities of the present invention are not limited to these options, but its scope is determined by the claims. In FIG. 1-10 depict fluidized bed thermal reaction devices according to embodiments of the present invention in which the present invention is presented as a combustion device, and FIG. 11 shows a thermal fluidized bed reaction device according to an embodiment of the present invention, in which the present invention is presented in the form of a gasification furnace (in the form of a gas generator). In these figures, the same or similar elements are indicated by the same reference numbers, and excessive explanation is omitted.

 FIG. 1 is a vertical sectional view schematically showing an essential part of a first embodiment of the present invention. In FIG. 1, a thermal fluidized bed reaction device has an opening 8 for discharging non-combustible components located in the center of the bottom of the furnace near the furnace 1 with a fluidized bed; a weak scattering plate 2 and a strong scattering plate 3, each of which is located between the non-combustible component outlet 8 and the side wall 42; a fuel supply opening 10 located above the weak diffusion plate 2; an inclined wall 9 located above the strong diffusion plate 3; and a protruding flange 44 mounted above the inclined wall 9. The flat configuration of the furnace may be rectangular or round. In furnace 1, a fluid containing non-combustible particles, such as sand, is blown by a fluidizing gas, such as air, an upward current blown into the furnace through a weak diffusion plate 2 and a strong diffusion plate 3. Consequently, the fluid is brought into a floating state, and thereby the main fluidized bed is formed. The variable upper surface 43 of the main fluidized bed is located at the height of the middle part of the inclined wall 9. To stimulate combustion, the oxygen content in the fluidizing gas is increased. However, by lowering the oxygen content in the fluidizing gas, a combustible substance can be gasified.

 Fluidizing gas from the gas source 14 is supplied to the weak diffusion chamber 4, which is located under the weak diffusion plate 2, through a pipe 62 and a connector 6. The fluidizing gas is supplied to the furnace at a relatively low fluidizing velocity through a large number of fluidizing gas supply holes 72 made in the plate 2 weak dispersion, so that a zone 17 of weak fluidization of the fluid is formed above it. In the low fluidization zone 17, a downward fluid flow is generated. The upper surface of the weak diffusion plate 2 is inclined downward so that it is lowered towards the non-combustible component outlet 8, as shown in a vertical section. As can be seen from FIG. 1, near the upper surface of the weak scattering plate 2, the downward flow 18 passes into an almost horizontal flow 19, following along the downwardly inclined surface.

 The strong diffusion plate 3 has a large number of fluidizing gas supply openings 74 and further comprises strong diffusion chambers 5 underneath. A fluidizing gas is supplied to the strong dispersion chamber 5 from the gas source 15 through a conduit 64 and a connector 7. The fluidizing gas is supplied to the furnace at a relatively high velocity of the fluidizing gas, so that the zone of strong fluidization of the fluid 16 over the strong diffusion plate 3 is formed. In the zone 16 of strong fluidization, an upward flow of 20 fluid is formed. The upper surface of the strong diffusion plate 3 is inclined upward so that the lowermost part is near the location of the non-combustible component outlet 8 and the surface rises toward the side wall 42, as shown in a vertical section.

 In FIG. 1, the fluid in the fluidized bed furnace 1 moves from the top of the upward stream 20 to the top of the weak fluidization zone 17, i.e. to the top of the downward flow 18, and then moves downward in the downward flow 18. Then, in the horizontal flow 19, the fluid moves to the bottom of the upward flow. The inclined wall is inclined in such a way that it is made higher towards the central part of the furnace, if we move from the side wall 42 of the furnace, as a result of which it reflects an upward flow into the region located above the weak diffusion plate 2.

 A combustible material supply opening 10 for loading combustible material 38 into the fluidized bed furnace 1 is located above the weak diffusion plate 2, as a result of which the combustible material falls into the region located above the weak dispersion plate 2. The combustible material 38 coming from the fuel supply opening 10 is mixed in the downward flow 18 of the fluid and moves down to the bottom of the furnace together with the downward flow 18, thereby undergoing thermal decomposition or partial combustion. Further, the combustible substance 38 is mixed in a horizontal fluid stream 19, following along the downwardly inclined surface of the weak dispersion plate 2, and then moves horizontally in the direction of the location of the outlet 8 of the non-combustible components. The combustible substance in the horizontal stream 19 is subjected to pneumatic elutriation and the action of gravitational separation of the fluidizing gas going up. As a result, the non-combustible components 11 of a large specific gravity move toward the lower side of the horizontal flow, while the combustible components of a small specific gravity are collected in the upper part of the horizontal flow. Therefore, an upper fluidized bed 12 with a low specific gravity and a high concentration of combustible components and a lower fluidized bed 13 with a high specific gravity and a high concentration of non-combustible components are formed near the outlet 8 of the output of non-combustible components.

 The upper fluidized bed 12 with a high concentration of combustible components is mixed in the upward flow 20 of the fluid passing over the outlet 8 of the output of non-combustible components, and burns under the influence of an oxidizing medium under conditions of strong fluidization. The flue gas generated in the fluidized bed rises to the protruding side 44 located above the upper surface 43 of the fluidized bed, and, if necessary, is subjected to secondary combustion. After that, dust removal and utilization of thermal energy are carried out, and then the flue gas is discharged into the atmosphere. Fluid and noncombustible components located in the lower fluidized bed 13 are removed through the outlet 8 of the output of noncombustible components. The passage 40, which communicates with the outlet 8 of the output of non-combustible components, allows the non-combustible substance and fluid to fall into the hole 8 of the output of non-combustible components discharged from the furnace through a hopper, discharge valve, etc. (not shown). The fluid removed from the furnace along with non-combustible components is removed by some means (not shown) and returned to the fluidized-bed furnace 1.

 In the thermal fluidized bed reaction apparatus shown in FIG. 1, the fluidizing gas is supplied from the gas source 15 to the passage 40 through the pipe 64, the exhaust pipe 66 and the nozzle 21. The fluidizing gas is blown up and follows in the furnace from the passage 40 through the outlet 8 of the non-combustible components, thereby achieving fluidization of the fluid above the outlet 8 non-combustible components, due to which the formation of the main fluidized bed, continuously following from the region located above the weak scattering plate 2, to the region located above the strong scattering plate 3, in as a result of which stabilization of the main circulating fluid flow occurs.

 The strong diffusion plate 3 has an upwardly inclined surface, which gradually rises with increasing distance from the non-combustible component outlet 8, as a result of which the upper fluidized bed 12 is separated from the horizontal flow 19, which moves approximately horizontally along the downwardly inclined surface of the weak diffusion plate 2 into the region the location of the outlet 8 of the output of non-combustible components, gradually passes into the upward stream 20, which ensures stabilization of the main circulating stream and preventing deposition of incombustible components on the strong diffusion plate 3. The device may also be such that the fluidizing velocity of the fluidizing gas supplied through the plate 3 strong dispersion, will gradually increase with increasing distance from the place of output of non-combustible components. The above contributes to the formation of the main circulating flow.

 FIG. 2 is a vertical sectional view schematically illustrating an essential part of a thermal fluidized bed reaction apparatus according to a second embodiment of the present invention. As shown in FIG. 2, the thermal fluidized bed reaction device comprises a weak dispersion plate 2 located in the center of the bottom of the fluidized bed furnace 1, auxiliary diffusion plates 3 ′ located respectively on both sides of the weak dispersion plate 2 and having a large number of fluidizing supply holes 76 gas; a non-combustible component outlet 8 and a strong diffusion plate 3 located between the auxiliary diffusion plates 3 'and the side wall 42; a fuel supply opening 10 located above the weak diffusion plate 2, inclined walls 9 located respectively above the strong dispersion plates; and a protruding flange located above the inclined walls 9.

 The upper surface of the weak scattering plate 2 is inclined downward so that its highest part is located in the center and lowers in the direction of the location of each outlet 8 of the output of non-combustible components. In the case where the horizontal section of the furnace is round, the upper surface of the weak scattering plate 2 is the surface of a circular cone. As shown in FIG. 2, the downward flow 18 is divided near the top 73 of the weak scattering plate 2 into two approximately horizontal flows 19, following along the left and right downward inclined surfaces. In the case where the horizontal section of the furnace is round, the upper surface of the strong diffusion plate 3 is the surface of the tilted cone, in which the outer peripheral edge is located above the inner peripheral edge.

 As shown in FIG. 2, the edge parts of the weak diffusion plate 2 are connected to the auxiliary diffusion plates 3 '. Fluidizing gas is supplied to the auxiliary dispersion chamber 5 ′ from the gas source 15 through a conduit 64, an outlet pipe 68, a valve 68 ′, and a connector 7 ′. The fluidizing gas is supplied to the furnace at a relatively high fluidization speed from the auxiliary diffusion chamber 5 ′ through the fluidizing gas supply openings 76 so that fluidization occurs over the auxiliary diffusion plate 3 ′.

 As shown in FIG. 2, the fluid in the fluidized-bed furnace 1 moves from the top of each upward flow 20 to the top of the weak fluidization zone 17, i.e. to the top of the downward flow 18, and then moves downward in the downward flow 18. Then, in each of the horizontal flows 19, the fluid moves to the bottom of each upward flow 20, thereby forming a main circulating flow. The downward flow 18, which contains the movable layer, is divided near the top 73 of the weak scattering plate 2 into horizontal flows 19 extending along the left and right downward inclined surfaces. In the case when the sectional plane of the furnace is rectangular, i.e. left and right, the main circulating flows are formed.

The horizontal flow above the weak scattering plate 2 is a moving bed in which the degree of fluidization of the fluid is low. Consequently, non-combustible components of extremely high specific gravity, for example iron, which are in a horizontal flow, also move without deposition at the bottom of the furnace. When the horizontal flow is over the auxiliary diffusion plate 3 ′, the moving bed passes into a fluidized bed in which the fluidizing velocity is high under the influence of the fluidizing gas supplied through the auxiliary diffusion plate 3 ′. Therefore, non-combustible components of high specific gravity quickly settle under the influence of pneumatic elutriation. Since the downward inclination angle of the auxiliary diffusion plate 3 ′ is steeper than that of the weak diffusion plate 2, the settling non-combustible components of high specific gravity are displaced to the output hole of the non-combustible components along the downward inclined surface of the auxiliary diffusion plate 3 'under the influence of gravity. The device shown in FIG. 2 is approximately identical to the device shown in FIG. 1, except that there are auxiliary diffusion plates 3 ′ and auxiliary diffusion chambers 5 ′ and that the weak diffusion plate 2, the non-combustible component exhaust holes and the strong plate
dispersions are located symmetrically relative to the center of the furnace. For this reason, further details are omitted.

 FIG. 3 is a vertical sectional view schematically illustrating an essential part of a thermal fluidized bed reaction apparatus according to a third embodiment of the present invention. As can be seen from FIG. 3, the tilt angle of each auxiliary diffusion plate 3 ′ is steeper than that of the angle shown in FIG. 2, and the lower edge 77 of the auxiliary diffusion plate 3 ′ extends, when viewed in plan, to the point of contact with the lower edge 75 of the adjacent strong diffusion plate 3, but is spaced from the edge 75 of the adjacent strong diffusion plate 3 in the vertical direction. The output of 8 non-combustible components is open at the location of the vertical gap between the two edges, i.e. It is open horizontally. Although the fluidizing gas is not supplied through the outlet 8 of the output of non-combustible components, the hole 8 does not interfere with the movement of the main circulating fluid flow, since the hole 8 of the output of non-combustible components has no clearance in plan and, therefore, does not interfere with the movement of the upward flow of the fluidizing gas. Structural elements of the rest of the device shown in FIG. 3 are approximately the same as those of the device shown in FIG. 1 or 2; for this reason, their description is omitted.

 FIG. 4 is a vertical sectional view of an essential part of a thermal fluidized bed reaction apparatus according to a thermal fluidized bed reaction apparatus according to a fourth embodiment of the present invention, in which each non-combustible component outlet 8 is horizontally open, as in the case of the apparatus shown in FIG. . 3, and the fluidizing gas is not supplied through the opening 8 of the output of non-combustible components. The device shown in FIG. 4 has heat recovery chambers 25, each of which is adjacent to the central part of the furnace, which forms the main combustion chamber, i.e. between the inclined wall 24 above the strong diffusion plate 3 and the side wall of the furnace 42, and the heat recovery device 27 is located in each heat recovery chamber 25. Each inclined wall 24 has a vertically extending lower portion. The third diffusion plates 28, which have approximately the same inclination as the strong diffusion plates 3, follow (each of them) from the outer edge connected with the strong diffusion plate 3 to the side wall 42 above the vertical projection of the inclined wall 24.

 The vertical clearance between the lower extension edge of the inclined wall 24 and the third diffusion plate 28 defines the lower connecting passage 29 between the central part of the furnace and the lower part of the heat recovery chamber 25. In addition, a plurality of vertically extending shielding tubes 23 are disposed between the upper end of the inclined wall 24 and the side wall of the furnace. The space between the shielding tubes 23 defines the upper connecting passage 23 ', which establishes a connection between the upper part of the heat recovery chamber 25 and the central part of the furnace. The gas source 32 and the third diffusion chamber 30, located under each third diffusion plate 28, communicate with each other through a pipe 68 ″ and a connector 31. Fluidizing gas is supplied to each heat recovery chamber 25 at a relatively low fluidizing velocity from the attached third chamber 30 dispersing through a large number of fluidizing gas supply openings 78 so that a downward subcirculating fluid stream 26 is formed.

 Part of the fluid in the upward stream 20, reflected to the central part of the furnace by each inclined wall 24, forms a return flow 22, which passes through the upper connecting passage 23 'above the inclined wall 24 and enters the upper part of the heat recovery chamber 25, where the fluid moves down in the form of a downward flow. The downward fluid flow then passes through the lower connecting passage 29 and is mixed in the upstream 20 of the main circulation stream to rise and reach the top of the upward flow 20. In this way, a subcirculating fluid stream 26 is passed through the heat recovery chamber. The fluid in the sub-circulation stream 26 is cooled by heat exchange with the heat recovery device 27 in the heat recovery chamber 25 and is heated by the heat of combustion in the upward stream 20. As shown in FIG. 10, the overall heat transfer coefficient of the heat recovery device varies greatly depending on the fluidizing velocity . Therefore, the amount of heat extracted can be effectively controlled by changing the speed of the fluidizing gas passing through the third diffusion plate 28.

 In the devices shown in FIG. 1 and 2, a fluidizing gas is supplied from a non-combustible component outlet 8, and the main fluidized bed does not contain a fracture portion. In the devices shown in FIG. 3 and 4, the edge of each auxiliary diffusion plate 3 ′ extends vertically from the edge of the adjacent strong diffusion plate, and the non-combustible component outlet 8 is obtained as a vertical gap between these two edges. Therefore, in the plan there is no rupture section at the fluidizing gas stream supplied upward from the bottom of the furnace. Thus, as with the devices shown in FIG. 1 and 2, a stable fluidized bed is formed.

 FIG. 5, 6, 7 are respectively views in space, plan, and section showing the bottom of a circular furnace in a thermal fluidized bed reaction device according to an embodiment of the present invention, which is equivalent to the case when in the embodiment shown in FIG. 2, the flat configuration of the furnace is replaced by a round. FIG. 7 is a sectional view taken along line AA shown in FIG. 6. That is, the weak diffusion plate 2 has a conical upper surface that is high in the center and low at the periphery. An annular auxiliary diffusion plate 3 ', four partially annular openings 8 of the output of non-combustible components and a strong diffusion plate 3 are concentrically relative to the weak dispersion plate 2. The inclined surface of the auxiliary scattering plate 3 'is steeper than the inclined surface of the weak scattering plate 2, which is located in the center. The strong diffusion plate 3 has an annular surface of an inverted cone that is low in the inner peripheral edge and high in the outer peripheral edge. The strong diffusion chamber 5 has an annular external shape.

 As shown in FIG. 5, 6 and 7, there are four partially annular openings 8 for the outlet of non-combustible components, and four fourth diffusion plates 3 ″ are located in a radial elongated position, each of which lies between a pair of adjacent holes for the outlet of non-combustible components. Each scattering plate 3 ″ of the fourth kind has two downward sloping surfaces going to the openings 8 of the output of non-combustible components lying on both sides of them. The downwardly sloping surfaces of the scattering plates 3 ″ of the fourth kind direct non-combustible components of large specific gravity to the holes 8 of the output of non-combustible components on the scattering plates 3 ″ of the fourth kind. Other structural elements and their functions with the device shown in FIG. 5, 6, and 7 are approximately the same as those of the embodiment illustrated in FIG. 2; for this reason, their description is omitted.

 FIG. 8 is a perspective view showing the bottom of a furnace of a thermal fluidized bed reaction apparatus according to a sixth embodiment of the present invention, which is equivalent to the case where the embodiment of FIG. 2 has a flat configuration of a furnace that is rectangular. As shown in FIG. 8, the weak diffusion plate 2 has a roof-shaped configuration that is rectangular in plan and which has a rib 73 'in the center. The weak diffusion plate 2, the auxiliary diffusion plates 3 ′, the non-combustible component outlet 8 and the strong diffusion plate 3 are symmetrically relative to the rib 73 ′, and they are all rectangular. The device shown in FIG. 8 comprises fourth diffusion plates 3 ″, which are perpendicular to the rib 73 ′ and parallel to the edges of the outlets 8 of the output of non-combustible components. The fourth diffuser plates 3 'have downward sloping surfaces extending to the associated openings 8 of the output of non-combustible components. The surfaces inclined downwardly at the fourth diffusion plates 3 ″ send non-combustible components of a large specific gravity to the openings 8 of the output of non-combustible components, thereby eliminating the deposition of non-combustible components on the fourth diffusion plates 3 ″. Other structural elements and their functions in this embodiment are approximately the same as in the embodiment shown in FIG. 2; for this reason, their description is omitted.

 FIG. 9 is a perspective view schematically showing the bottom of a furnace of a thermal fluidized bed reaction apparatus according to a seventh embodiment of the present invention, which is equivalent to the case where the embodiment shown in FIG. 2, the flat configuration of the furnace is rectangular. This embodiment has approximately the same device as the embodiment shown in FIG. 8, but with the difference that the edge of each strong diffusion plate 3, which is adjacent to adjacent non-combustible component output holes 8, lies in the plane of continuation of the inclined surface of the weak diffusion plate 2, while the edge of each strong diffusion plate 3, which is adjacent to the side wall , is located above the continuation plane of the inclined surface of the weak scattering plate 2. Other structural elements and their functions in this embodiment are approximately the same as in the embodiment shown in FIG. 2 or 8; for this reason, their description is omitted. The devices shown in FIG. 8 and 9, have a relatively small number of curved sections, and, therefore, they are relatively simple in terms of design and manufacture. Accordingly, their manufacturing cost is low.

 FIG. 10 is a graph of the total heat transfer coefficient of a heat recovery device versus the fluidization rate of a fluidizing gas supplied through a third diffusion plate 28 in a thermal fluidized bed reaction apparatus of the present invention. When the fluidizing velocity is in the range from 0 to 0.3 m / s, in particular from 0.05 to 0.25 m / s, the total heat transfer coefficient of the heat recovery device varies significantly with the change in the fluidizing velocity. Accordingly, if the total heat transfer coefficient is changed by adjusting the fluidizing velocity in the heat recovery chamber in the indicated range of the fluidizing velocity, then the amount of heat utilized can be controlled over a wide range.

FIG. 11 is a cross-sectional view schematically illustrating a thermal fluidized bed reaction apparatus according to an eighth embodiment of the present invention, which in design is an alloy burning furnace 90 connected to a thermal fluidized bed reaction apparatus. The thermal fluidized bed reaction device has the same construction as the device shown in FIG. 2, but with the difference that it acts as a gasification furnace. The product obtained in the fluidized bed furnace 1, which contains combustible gas, light and finely divided uncombusted components such as coal and tar, fly ash, etc., is sent to a vertical primary combustion chamber 82 of a cylindrical shape of an alloy burning furnace 90, where the product is burned and the ash is melted during its subsequent processing at a high temperature of about 1350 ^o C, for example, when secondary air or oxygen is added thereto, it is then burnt and the ash is melted in an inclined secondary combustion chamber 84. The result exhaust flue gas 93 and fused slag 95 are separated in the exhaust chamber 92 and discharged separately. Secondary combustion chamber 84 is installed if necessary.

 The present invention has the following principal technical solutions and advantages.

 1. In a technical fluidized bed reaction device, a main circulating stream is formed containing a downward flow and an upward flow of fluid, and the combustible material is discharged into the upper part of the downward flow, mixed in the main circulating flow and burned. Accordingly, it is possible to burn or gasify a uniformly and efficiently combustible substance, such as waste, which is characterized by variability with respect to size, content of non-combustible components, specific gravity, etc.

 2. The combustible substance moves in a downward and horizontal flow, being subjected to combustion, decomposition and gasification, and non-combustible components of large specific gravity are directed to the place of removal of non-combustible components along the inclined surface of the weak dispersion plate, subject to the gradual release of small specific gravity from combustible components under the influence of pneumatic elutriation and gravitational separating action of the fluidizing gas. In the place of non-combustible components, combustible components settle and separate under the influence of gravitational separation and are unloaded from the furnace evenly. Consequently, non-combustible components will not be deposited at the bottom of the furnace, and non-combustible components will create a minimum of inconvenience to the supply of fluidizing gas, combustion or gasification, heat recovery, etc. In addition, the recovered non-combustible components can be easily processed since they have a low combustible content.

 3. Part of the fluidizing gas is supplied from the outlet of the outlet of non-combustible components or the outlet of the outlet of non-combustible components is made open horizontally and not vertically. Accordingly, fluidizing gas is supplied from the entire bottom surface of the furnace and thereby forms a stable main circulating stream. Therefore, it is possible to burn or gasify a combustible substance evenly and efficiently, and the device is provided with the ability to work without interruptions. It turns out to be possible to carry out complete combustion or highly efficient gasification of a combustible substance by controlled combustion of a certain amount of air.

 4. A heat recovery chamber is formed between the inclined wall and the side wall of the furnace, and a third diffusion plate is placed under the heat recovery chamber. The third diffusion plate has approximately the same inclination as the strong diffusion plate, and moreover, the surface inclined downward goes towards the outlet of non-combustible components. Therefore, non-combustible components located in the heat recovery chamber are uniformly directed to the outlet of the output of non-combustible components without disrupting the heat recovery process. In addition, the heat transfer coefficient of the heat recovery device can be changed to a significant extent by controlling the flow of fluidizing gas supplied through a third diffusion plate. For this reason, it is possible to easily control the amount of heat recovered.

Claims (8)

 1. Thermal fluidized bed reaction device in which a combustible substance containing non-combustible components is burned or gasified in a fluidized bed furnace, characterized in that the weak diffusion plate and strong dispersion plate, each of which contains a large number of fluidizing gas supply openings, located in the bottom of the furnace; a non-combustible component outlet opening is disposed between the weak diffusion plate and the strong dispersion plate; a fuel supply opening is positioned so that the combustible material can be discharged into the region above the weak diffusion plate; the weak dispersion plate is capable of supplying a fluidizing gas so that a relatively low fluidizing velocity is established at the fluid and a downward flow of fluid is formed, the weak dispersion plate having a downward inclined surface extending toward the outlet of non-combustible components; the strong diffusion plate is capable of supplying a fluidizing gas in such a way that a relatively high fluidization rate is established for the fluid and an upward flow of fluid is formed, and a part of the fluidizing gas is supplied to the furnace through a non-combustible component outlet, and an auxiliary diffusion plate having a large number of supply openings fluidizing gas, is located between the aforementioned plate of weak dispersion and the hole of the output of non-combustible components, and auxiliary The diffusion plate is capable of supplying a fluidizing gas so that a relatively high fluidizing velocity is imparted to the fluid, the auxiliary diffusion plate having a sloping surface with a sharper slope than that of the weak diffusion plate, in the region between the lower edge of the weak diffusion plate and the non-combustible outlet components, so that the downward inclined surface follows to the opening of the output of non-combustible components.  2. The thermal fluidized bed reaction device according to claim 1, characterized in that the inclined wall is located above said strong diffusion plate so that the fluidized gas and fluid rising above the strong diffusion plate are reflected towards the center of the furnace, and in which the strong diffusion plate has a surface inclined upwards, which gradually increases with increasing distance from the outlet of the non-combustible components, and the strong diffusion plate is located Thus, the fluidizing velocity gradually increases with increasing distance from the outlet of the outlet of non-combustible components, while the heat recovery chamber is formed between the inclined wall and the side wall of the furnace, and the heat recovery chamber communicates with the central part of the furnace at the upper and lower ends of the inclined wall, and wherein the heat recovery device is positioned between the strong diffusion plate and the side wall of the furnace so that the third diffusion plate is adjacent to the outer edge of the plate ins strong dispersion, the third diffusion plate is capable of supplying a fluidizing gas so that the relatively low fluidizing velocity in fluid medium in the heat recovery chamber, the third diffusion plate has an upward slant surface with the same slope as that of the strong diffusion plate.  3. Thermal fluidized bed reaction device according to claim 1 or 2, characterized in that the bottom of the said fluidized bed furnace and the weak dispersion plate are each approximately circular in shape and in which the weak dispersion plate has a conical shape, in which the center is round the part is high and the peripheral edge of the round part is low; the output hole of non-combustible components has a configuration in the form of a set of partially annular portions concentrically mounted relative to the weak diffusion plate, and the strong diffusion plate is circular and is concentrically relative to the weak diffusion plate.  4. Thermal fluidized bed reaction device in which a combustible substance containing non-combustible components is burned or gasified in a fluidized bed furnace, characterized in that the weak diffusion plate, auxiliary diffusion plate and strong dispersion plate, each of which has a large number of openings fluidizing gas feeds are located in the bottom of the furnace; a non-combustible component outlet opening is located between the auxiliary diffusion plate and the strong diffusion plate; a hole for supplying a combustible substance is positioned so that the combustible substance can fall into the region above the weak dispersion plate; the weak dispersion plate is capable of supplying a fluidizing gas so that a relatively low fluidizing velocity is imparted to the fluid and a downward flow of fluid is generated, the weak dispersion plate having a downward inclined surface extending to the outlet of non-combustible components; the auxiliary dispersion plate is capable of supplying a fluidizing gas so that a relatively high fluidizing velocity is imparted to the fluid, the auxiliary dispersion plate having a sloping surface with a steeper slope than that of the weak dispersion plate, in the region between the lower edge of the weak dispersion plate and the non-combustible discharge opening components, so that the downward inclined surface extends to a non-combustible component outlet; the strong diffusion plate has the ability to supply fluidizing gas so that a relatively high fluidizing velocity is communicated to the fluid and an upward flow of fluid is formed; the lower edge of the downwardly inclined surface of the auxiliary diffusion plate substantially contacts, in plan, the edge of the adjacent strong diffusion plate and these edges extend from each other in the vertical direction and the outlet of the incombustible components is open in the form of a vertical gap between the two edges.  5. Thermal fluidized bed reaction device according to claim 4, characterized in that the inclined wall is located above the strong diffusion plate to reflect the fluidized gas and fluid rising above the strong diffusion plate to the central part of the furnace and in which the strong diffusion plate has an inclined upward surface, which gradually increases with increasing distance from the outlet of the exit of non-combustible components, and the plate of strong dispersion is located so that the fluidizing velocity spine progressively increases with increasing distance from the incombustible component outlet.  6. Thermal fluidized bed reaction device according to claim 4 or 5, characterized in that the heat recovery chamber is formed between the said inclined wall and the side wall of the furnace, the heat recovery chamber communicating with the Central part of the furnace at the upper and lower ends of the inclined wall, and in which the heat recovery device is located in the heat recovery chamber and the third diffusion plate is located between the strong diffusion plate and the side wall of the furnace, so that the third diffusion plate is in contact it is connected to the outer edge of the strong diffusion plate, the third diffusion plate being able to supply fluidizing gas in such a way that a relatively low fluidizing velocity is imparted to the fluid in the heat recovery chamber, and the third diffusing plate has an inclined surface upward with approximately the same inclination as the plate strong dispersion.  7. Thermal fluidized bed reaction device according to any one of paragraphs. 4 - 6, characterized in that the bottom of the said fluidized bed furnace and the weak dispersion plate are each approximately circular in plan and in which the weak dispersion plate has a conical shape, in which the center of the central part is high and the peripheral edge of the central part is low; the outlet of the incombustible components has a configuration of a plurality of partially annular portions concentrically disposed relative to the weak scattering plate, and the strong scattering plate is annular and arranged concentrically with respect to the weak scattering plate.  8. Thermal fluidized bed reaction device according to any one of claims 4 to 7, characterized in that the fluidizing gas is a gas of the same nature or a combination of a number of gases selected from the group consisting of air, steam, oxygen or exhaust gas.

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